EP0367445B1 - Extruder polymerization of polyurethanes - Google Patents
Extruder polymerization of polyurethanes Download PDFInfo
- Publication number
- EP0367445B1 EP0367445B1 EP89310721A EP89310721A EP0367445B1 EP 0367445 B1 EP0367445 B1 EP 0367445B1 EP 89310721 A EP89310721 A EP 89310721A EP 89310721 A EP89310721 A EP 89310721A EP 0367445 B1 EP0367445 B1 EP 0367445B1
- Authority
- EP
- European Patent Office
- Prior art keywords
- extruder
- diol
- diisocyanate
- weight percent
- polymer
- Prior art date
- Legal status (The legal status is an assumption and is not a legal conclusion. Google has not performed a legal analysis and makes no representation as to the accuracy of the status listed.)
- Expired - Lifetime
Links
- 239000004814 polyurethane Substances 0.000 title claims description 33
- 229920002635 polyurethane Polymers 0.000 title claims description 33
- 238000006116 polymerization reaction Methods 0.000 title claims description 6
- 150000002009 diols Chemical class 0.000 claims description 66
- -1 aromatic glycols Chemical class 0.000 claims description 46
- 238000000034 method Methods 0.000 claims description 35
- 239000012948 isocyanate Substances 0.000 claims description 33
- 150000002513 isocyanates Chemical class 0.000 claims description 33
- 229920000642 polymer Polymers 0.000 claims description 31
- WERYXYBDKMZEQL-UHFFFAOYSA-N butane-1,4-diol Chemical compound OCCCCO WERYXYBDKMZEQL-UHFFFAOYSA-N 0.000 claims description 28
- 239000000178 monomer Substances 0.000 claims description 25
- LYCAIKOWRPUZTN-UHFFFAOYSA-N Ethylene glycol Chemical compound OCCO LYCAIKOWRPUZTN-UHFFFAOYSA-N 0.000 claims description 20
- 125000005442 diisocyanate group Chemical group 0.000 claims description 20
- 238000006243 chemical reaction Methods 0.000 claims description 18
- NIXOWILDQLNWCW-UHFFFAOYSA-M Acrylate Chemical compound [O-]C(=O)C=C NIXOWILDQLNWCW-UHFFFAOYSA-M 0.000 claims description 15
- KORSJDCBLAPZEQ-UHFFFAOYSA-N dicyclohexylmethane-4,4'-diisocyanate Chemical compound C1CC(N=C=O)CCC1CC1CCC(N=C=O)CC1 KORSJDCBLAPZEQ-UHFFFAOYSA-N 0.000 claims description 15
- 125000002887 hydroxy group Chemical group [H]O* 0.000 claims description 15
- 230000005855 radiation Effects 0.000 claims description 15
- CERQOIWHTDAKMF-UHFFFAOYSA-M methacrylate group Chemical group C(C(=C)C)(=O)[O-] CERQOIWHTDAKMF-UHFFFAOYSA-M 0.000 claims description 11
- 239000002994 raw material Substances 0.000 claims description 11
- 125000004432 carbon atom Chemical group C* 0.000 claims description 10
- WGCNASOHLSPBMP-UHFFFAOYSA-N hydroxyacetaldehyde Natural products OCC=O WGCNASOHLSPBMP-UHFFFAOYSA-N 0.000 claims description 10
- 229920000728 polyester Polymers 0.000 claims description 9
- 125000001931 aliphatic group Chemical group 0.000 claims description 8
- UHOVQNZJYSORNB-UHFFFAOYSA-N Benzene Chemical compound C1=CC=CC=C1 UHOVQNZJYSORNB-UHFFFAOYSA-N 0.000 claims description 6
- 239000004970 Chain extender Substances 0.000 claims description 6
- MTHSVFCYNBDYFN-UHFFFAOYSA-N diethylene glycol Chemical compound OCCOCCO MTHSVFCYNBDYFN-UHFFFAOYSA-N 0.000 claims description 6
- 125000001495 ethyl group Chemical group [H]C([H])([H])C([H])([H])* 0.000 claims description 6
- 150000008064 anhydrides Chemical class 0.000 claims description 5
- 238000012662 bulk polymerization Methods 0.000 claims description 5
- 239000005058 Isophorone diisocyanate Substances 0.000 claims description 4
- 238000001816 cooling Methods 0.000 claims description 4
- NIMLQBUJDJZYEJ-UHFFFAOYSA-N isophorone diisocyanate Chemical compound CC1(C)CC(N=C=O)CC(C)(CN=C=O)C1 NIMLQBUJDJZYEJ-UHFFFAOYSA-N 0.000 claims description 4
- 229920001296 polysiloxane Polymers 0.000 claims description 4
- IUGOPULVANEDRX-UHFFFAOYSA-N 2-ethylhexane-1,1-diol Chemical compound CCCCC(CC)C(O)O IUGOPULVANEDRX-UHFFFAOYSA-N 0.000 claims description 3
- 238000004566 IR spectroscopy Methods 0.000 claims description 3
- 238000006446 extruder reaction Methods 0.000 claims description 3
- XXMIOPMDWAUFGU-UHFFFAOYSA-N hexane-1,6-diol Chemical compound OCCCCCCO XXMIOPMDWAUFGU-UHFFFAOYSA-N 0.000 claims description 3
- ORTVZLZNOYNASJ-UPHRSURJSA-N (z)-but-2-ene-1,4-diol Chemical compound OC\C=C/CO ORTVZLZNOYNASJ-UPHRSURJSA-N 0.000 claims description 2
- 239000005059 1,4-Cyclohexyldiisocyanate Substances 0.000 claims description 2
- VLVVSHOQIJBJAG-UHFFFAOYSA-N 1,6-diisocyanato-2,2,4,4-tetramethylhexane Chemical compound O=C=NCCC(C)(C)CC(C)(C)CN=C=O VLVVSHOQIJBJAG-UHFFFAOYSA-N 0.000 claims description 2
- QGLRLXLDMZCFBP-UHFFFAOYSA-N 1,6-diisocyanato-2,4,4-trimethylhexane Chemical compound O=C=NCC(C)CC(C)(C)CCN=C=O QGLRLXLDMZCFBP-UHFFFAOYSA-N 0.000 claims description 2
- 239000005977 Ethylene Substances 0.000 claims description 2
- IAYPIBMASNFSPL-UHFFFAOYSA-N Ethylene oxide Chemical compound C1CO1 IAYPIBMASNFSPL-UHFFFAOYSA-N 0.000 claims description 2
- 239000005057 Hexamethylene diisocyanate Substances 0.000 claims description 2
- NINIDFKCEFEMDL-UHFFFAOYSA-N Sulfur Chemical compound [S] NINIDFKCEFEMDL-UHFFFAOYSA-N 0.000 claims description 2
- ORLQHILJRHBSAY-UHFFFAOYSA-N [1-(hydroxymethyl)cyclohexyl]methanol Chemical compound OCC1(CO)CCCCC1 ORLQHILJRHBSAY-UHFFFAOYSA-N 0.000 claims description 2
- 150000001252 acrylic acid derivatives Chemical class 0.000 claims description 2
- QVGXLLKOCUKJST-UHFFFAOYSA-N atomic oxygen Chemical compound [O] QVGXLLKOCUKJST-UHFFFAOYSA-N 0.000 claims description 2
- 229910052799 carbon Inorganic materials 0.000 claims description 2
- 150000001875 compounds Chemical class 0.000 claims description 2
- 150000001991 dicarboxylic acids Chemical class 0.000 claims description 2
- KIQKWYUGPPFMBV-UHFFFAOYSA-N diisocyanatomethane Chemical compound O=C=NCN=C=O KIQKWYUGPPFMBV-UHFFFAOYSA-N 0.000 claims description 2
- 150000002148 esters Chemical class 0.000 claims description 2
- RRAMGCGOFNQTLD-UHFFFAOYSA-N hexamethylene diisocyanate Chemical compound O=C=NCCCCCCN=C=O RRAMGCGOFNQTLD-UHFFFAOYSA-N 0.000 claims description 2
- 229910052760 oxygen Inorganic materials 0.000 claims description 2
- 239000001301 oxygen Substances 0.000 claims description 2
- QQONPFPTGQHPMA-UHFFFAOYSA-N propylene Natural products CC=C QQONPFPTGQHPMA-UHFFFAOYSA-N 0.000 claims description 2
- 150000003457 sulfones Chemical class 0.000 claims description 2
- 229910052717 sulfur Inorganic materials 0.000 claims description 2
- 239000011593 sulfur Substances 0.000 claims description 2
- 150000002734 metacrylic acid derivatives Chemical class 0.000 claims 1
- 239000010408 film Substances 0.000 description 43
- FXHOOIRPVKKKFG-UHFFFAOYSA-N N,N-Dimethylacetamide Chemical compound CN(C)C(C)=O FXHOOIRPVKKKFG-UHFFFAOYSA-N 0.000 description 17
- 229940113088 dimethylacetamide Drugs 0.000 description 17
- 239000008188 pellet Substances 0.000 description 17
- 239000000376 reactant Substances 0.000 description 17
- NWVVVBRKAWDGAB-UHFFFAOYSA-N p-methoxyphenol Chemical compound COC1=CC=C(O)C=C1 NWVVVBRKAWDGAB-UHFFFAOYSA-N 0.000 description 13
- 229920003224 poly(trimethylene oxide) Polymers 0.000 description 13
- UKLDJPRMSDWDSL-UHFFFAOYSA-L [dibutyl(dodecanoyloxy)stannyl] dodecanoate Chemical compound CCCCCCCCCCCC(=O)O[Sn](CCCC)(CCCC)OC(=O)CCCCCCCCCCC UKLDJPRMSDWDSL-UHFFFAOYSA-L 0.000 description 11
- 239000012975 dibutyltin dilaurate Substances 0.000 description 11
- XITRBUPOXXBIJN-UHFFFAOYSA-N bis(2,2,6,6-tetramethylpiperidin-4-yl) decanedioate Chemical compound C1C(C)(C)NC(C)(C)CC1OC(=O)CCCCCCCCC(=O)OC1CC(C)(C)NC(C)(C)C1 XITRBUPOXXBIJN-UHFFFAOYSA-N 0.000 description 10
- OIWOHHBRDFKZNC-UHFFFAOYSA-N cyclohexyl 2-methylprop-2-enoate Chemical compound CC(=C)C(=O)OC1CCCCC1 OIWOHHBRDFKZNC-UHFFFAOYSA-N 0.000 description 10
- 239000000203 mixture Substances 0.000 description 10
- 229920006267 polyester film Polymers 0.000 description 8
- 238000003825 pressing Methods 0.000 description 8
- 239000000463 material Substances 0.000 description 6
- 239000004721 Polyphenylene oxide Substances 0.000 description 5
- 150000002334 glycols Chemical class 0.000 description 5
- 238000010438 heat treatment Methods 0.000 description 5
- 239000012299 nitrogen atmosphere Substances 0.000 description 5
- 229920000570 polyether Polymers 0.000 description 5
- 239000000126 substance Substances 0.000 description 5
- XLYOFNOQVPJJNP-UHFFFAOYSA-N water Substances O XLYOFNOQVPJJNP-UHFFFAOYSA-N 0.000 description 5
- 239000000654 additive Substances 0.000 description 4
- 238000001125 extrusion Methods 0.000 description 4
- 238000010791 quenching Methods 0.000 description 4
- RTZKZFJDLAIYFH-UHFFFAOYSA-N Diethyl ether Chemical compound CCOCC RTZKZFJDLAIYFH-UHFFFAOYSA-N 0.000 description 3
- 125000000732 arylene group Chemical group 0.000 description 3
- ISAOCJYIOMOJEB-UHFFFAOYSA-N benzoin Chemical compound C=1C=CC=CC=1C(O)C(=O)C1=CC=CC=C1 ISAOCJYIOMOJEB-UHFFFAOYSA-N 0.000 description 3
- 239000003153 chemical reaction reagent Substances 0.000 description 3
- 238000010894 electron beam technology Methods 0.000 description 3
- 229920006264 polyurethane film Polymers 0.000 description 3
- 238000002360 preparation method Methods 0.000 description 3
- IJGRMHOSHXDMSA-UHFFFAOYSA-N Atomic nitrogen Chemical compound N#N IJGRMHOSHXDMSA-UHFFFAOYSA-N 0.000 description 2
- OWYWGLHRNBIFJP-UHFFFAOYSA-N Ipazine Chemical compound CCN(CC)C1=NC(Cl)=NC(NC(C)C)=N1 OWYWGLHRNBIFJP-UHFFFAOYSA-N 0.000 description 2
- 235000000126 Styrax benzoin Nutrition 0.000 description 2
- 244000028419 Styrax benzoin Species 0.000 description 2
- 235000008411 Sumatra benzointree Nutrition 0.000 description 2
- WYURNTSHIVDZCO-UHFFFAOYSA-N Tetrahydrofuran Chemical compound C1CCOC1 WYURNTSHIVDZCO-UHFFFAOYSA-N 0.000 description 2
- 125000002947 alkylene group Chemical group 0.000 description 2
- 125000003118 aryl group Chemical group 0.000 description 2
- 229960002130 benzoin Drugs 0.000 description 2
- 230000015572 biosynthetic process Effects 0.000 description 2
- 239000003054 catalyst Substances 0.000 description 2
- 239000013068 control sample Substances 0.000 description 2
- 125000002993 cycloalkylene group Chemical group 0.000 description 2
- 230000003247 decreasing effect Effects 0.000 description 2
- 239000004205 dimethyl polysiloxane Substances 0.000 description 2
- 238000006073 displacement reaction Methods 0.000 description 2
- 238000009826 distribution Methods 0.000 description 2
- 238000002474 experimental method Methods 0.000 description 2
- 235000019382 gum benzoic Nutrition 0.000 description 2
- 238000002329 infrared spectrum Methods 0.000 description 2
- 238000002156 mixing Methods 0.000 description 2
- 230000000704 physical effect Effects 0.000 description 2
- 229920003023 plastic Polymers 0.000 description 2
- 239000004033 plastic Substances 0.000 description 2
- 229920000435 poly(dimethylsiloxane) Polymers 0.000 description 2
- 229920000515 polycarbonate Polymers 0.000 description 2
- 239000004417 polycarbonate Substances 0.000 description 2
- 239000003381 stabilizer Substances 0.000 description 2
- 125000005717 substituted cycloalkylene group Chemical group 0.000 description 2
- 229920002818 (Hydroxyethyl)methacrylate Polymers 0.000 description 1
- ALQLPWJFHRMHIU-UHFFFAOYSA-N 1,4-diisocyanatobenzene Chemical compound O=C=NC1=CC=C(N=C=O)C=C1 ALQLPWJFHRMHIU-UHFFFAOYSA-N 0.000 description 1
- AXKZIDYFAMKWSA-UHFFFAOYSA-N 1,6-dioxacyclododecane-7,12-dione Chemical compound O=C1CCCCC(=O)OCCCCO1 AXKZIDYFAMKWSA-UHFFFAOYSA-N 0.000 description 1
- QRIMLDXJAPZHJE-UHFFFAOYSA-N 2,3-dihydroxypropyl 2-methylprop-2-enoate Chemical compound CC(=C)C(=O)OCC(O)CO QRIMLDXJAPZHJE-UHFFFAOYSA-N 0.000 description 1
- ZMWRRFHBXARRRT-UHFFFAOYSA-N 2-(benzotriazol-2-yl)-4,6-bis(2-methylbutan-2-yl)phenol Chemical compound CCC(C)(C)C1=CC(C(C)(C)CC)=CC(N2N=C3C=CC=CC3=N2)=C1O ZMWRRFHBXARRRT-UHFFFAOYSA-N 0.000 description 1
- DBBSWURSQHDBEQ-UHFFFAOYSA-N 2-butan-2-yloxy-1,2-diphenylethanone Chemical compound C=1C=CC=CC=1C(OC(C)CC)C(=O)C1=CC=CC=C1 DBBSWURSQHDBEQ-UHFFFAOYSA-N 0.000 description 1
- UPMLOUAZCHDJJD-UHFFFAOYSA-N 4,4'-Diphenylmethane Diisocyanate Chemical compound C1=CC(N=C=O)=CC=C1CC1=CC=C(N=C=O)C=C1 UPMLOUAZCHDJJD-UHFFFAOYSA-N 0.000 description 1
- ZRWNRAJCPNLYAK-UHFFFAOYSA-N 4-bromobenzamide Chemical compound NC(=O)C1=CC=C(Br)C=C1 ZRWNRAJCPNLYAK-UHFFFAOYSA-N 0.000 description 1
- VTLYFUHAOXGGBS-UHFFFAOYSA-N Fe3+ Chemical class [Fe+3] VTLYFUHAOXGGBS-UHFFFAOYSA-N 0.000 description 1
- 239000004606 Fillers/Extenders Substances 0.000 description 1
- WOBHKFSMXKNTIM-UHFFFAOYSA-N Hydroxyethyl methacrylate Chemical compound CC(=C)C(=O)OCCO WOBHKFSMXKNTIM-UHFFFAOYSA-N 0.000 description 1
- 229920001410 Microfiber Polymers 0.000 description 1
- WMTLVUCMBWBYSO-UHFFFAOYSA-N N=C=O.N=C=O.C=1C=CC=CC=1OC1=CC=CC=C1 Chemical compound N=C=O.N=C=O.C=1C=CC=CC=1OC1=CC=CC=C1 WMTLVUCMBWBYSO-UHFFFAOYSA-N 0.000 description 1
- 229920003171 Poly (ethylene oxide) Polymers 0.000 description 1
- 239000005062 Polybutadiene Substances 0.000 description 1
- 239000004433 Thermoplastic polyurethane Substances 0.000 description 1
- ATJFFYVFTNAWJD-UHFFFAOYSA-N Tin Chemical compound [Sn] ATJFFYVFTNAWJD-UHFFFAOYSA-N 0.000 description 1
- 239000002253 acid Substances 0.000 description 1
- 150000007513 acids Chemical class 0.000 description 1
- 229920003054 adipate polyester Polymers 0.000 description 1
- 238000013019 agitation Methods 0.000 description 1
- 150000001299 aldehydes Chemical class 0.000 description 1
- 125000002723 alicyclic group Chemical group 0.000 description 1
- 150000001350 alkyl halides Chemical class 0.000 description 1
- XAGFODPZIPBFFR-UHFFFAOYSA-N aluminium Chemical compound [Al] XAGFODPZIPBFFR-UHFFFAOYSA-N 0.000 description 1
- 229910052782 aluminium Inorganic materials 0.000 description 1
- 238000004458 analytical method Methods 0.000 description 1
- WURBFLDFSFBTLW-UHFFFAOYSA-N benzil Chemical compound C=1C=CC=CC=1C(=O)C(=O)C1=CC=CC=C1 WURBFLDFSFBTLW-UHFFFAOYSA-N 0.000 description 1
- 239000011230 binding agent Substances 0.000 description 1
- 230000005540 biological transmission Effects 0.000 description 1
- 229920001400 block copolymer Polymers 0.000 description 1
- 238000009835 boiling Methods 0.000 description 1
- 239000001273 butane Substances 0.000 description 1
- CDQSJQSWAWPGKG-UHFFFAOYSA-N butane-1,1-diol Chemical compound CCCC(O)O CDQSJQSWAWPGKG-UHFFFAOYSA-N 0.000 description 1
- 125000003178 carboxy group Chemical group [H]OC(*)=O 0.000 description 1
- 239000000470 constituent Substances 0.000 description 1
- 238000010924 continuous production Methods 0.000 description 1
- 239000002826 coolant Substances 0.000 description 1
- 239000012809 cooling fluid Substances 0.000 description 1
- 229920001577 copolymer Polymers 0.000 description 1
- 238000004132 cross linking Methods 0.000 description 1
- 125000004122 cyclic group Chemical group 0.000 description 1
- FOTKYAAJKYLFFN-UHFFFAOYSA-N decane-1,10-diol Chemical compound OCCCCCCCCCCO FOTKYAAJKYLFFN-UHFFFAOYSA-N 0.000 description 1
- 230000007423 decrease Effects 0.000 description 1
- 230000018044 dehydration Effects 0.000 description 1
- 238000006297 dehydration reaction Methods 0.000 description 1
- 230000001419 dependent effect Effects 0.000 description 1
- AYOHIQLKSOJJQH-UHFFFAOYSA-N dibutyltin Chemical compound CCCC[Sn]CCCC AYOHIQLKSOJJQH-UHFFFAOYSA-N 0.000 description 1
- ZBCBWPMODOFKDW-UHFFFAOYSA-N diethanolamine Chemical compound OCCNCCO ZBCBWPMODOFKDW-UHFFFAOYSA-N 0.000 description 1
- PWEVMPIIOJUPRI-UHFFFAOYSA-N dimethyltin Chemical compound C[Sn]C PWEVMPIIOJUPRI-UHFFFAOYSA-N 0.000 description 1
- 150000002019 disulfides Chemical class 0.000 description 1
- 238000005516 engineering process Methods 0.000 description 1
- HQPMKSGTIOYHJT-UHFFFAOYSA-N ethane-1,2-diol;propane-1,2-diol Chemical compound OCCO.CC(O)CO HQPMKSGTIOYHJT-UHFFFAOYSA-N 0.000 description 1
- 239000000835 fiber Substances 0.000 description 1
- 239000003112 inhibitor Substances 0.000 description 1
- 239000003999 initiator Substances 0.000 description 1
- 229910001410 inorganic ion Inorganic materials 0.000 description 1
- 150000002576 ketones Chemical class 0.000 description 1
- 238000004898 kneading Methods 0.000 description 1
- 239000004611 light stabiliser Substances 0.000 description 1
- 239000007788 liquid Substances 0.000 description 1
- RBQRWNWVPQDTJJ-UHFFFAOYSA-N methacryloyloxyethyl isocyanate Chemical compound CC(=C)C(=O)OCCN=C=O RBQRWNWVPQDTJJ-UHFFFAOYSA-N 0.000 description 1
- 239000003658 microfiber Substances 0.000 description 1
- OFBQJSOFQDEBGM-UHFFFAOYSA-N n-pentane Natural products CCCCC OFBQJSOFQDEBGM-UHFFFAOYSA-N 0.000 description 1
- 229910052757 nitrogen Inorganic materials 0.000 description 1
- BDJRBEYXGGNYIS-UHFFFAOYSA-N nonanedioic acid Chemical compound OC(=O)CCCCCCCC(O)=O BDJRBEYXGGNYIS-UHFFFAOYSA-N 0.000 description 1
- 239000003960 organic solvent Substances 0.000 description 1
- 125000002524 organometallic group Chemical group 0.000 description 1
- 238000005453 pelletization Methods 0.000 description 1
- 150000002978 peroxides Chemical class 0.000 description 1
- 239000003504 photosensitizing agent Substances 0.000 description 1
- 150000003022 phthalic acids Chemical class 0.000 description 1
- 229920000233 poly(alkylene oxides) Polymers 0.000 description 1
- 229920000058 polyacrylate Polymers 0.000 description 1
- 229920002857 polybutadiene Polymers 0.000 description 1
- 229920001610 polycaprolactone Polymers 0.000 description 1
- 239000004632 polycaprolactone Substances 0.000 description 1
- 229920000098 polyolefin Polymers 0.000 description 1
- 229920001451 polypropylene glycol Polymers 0.000 description 1
- 230000002028 premature Effects 0.000 description 1
- 238000012545 processing Methods 0.000 description 1
- 230000001681 protective effect Effects 0.000 description 1
- 238000005086 pumping Methods 0.000 description 1
- 238000010926 purge Methods 0.000 description 1
- 238000010526 radical polymerization reaction Methods 0.000 description 1
- 150000003254 radicals Chemical class 0.000 description 1
- 230000009257 reactivity Effects 0.000 description 1
- 238000012827 research and development Methods 0.000 description 1
- 239000011347 resin Substances 0.000 description 1
- 229920005989 resin Polymers 0.000 description 1
- 239000000523 sample Substances 0.000 description 1
- 241000894007 species Species 0.000 description 1
- 238000003756 stirring Methods 0.000 description 1
- 238000003860 storage Methods 0.000 description 1
- 150000003462 sulfoxides Chemical class 0.000 description 1
- 238000003786 synthesis reaction Methods 0.000 description 1
- 238000012360 testing method Methods 0.000 description 1
- YLQBMQCUIZJEEH-UHFFFAOYSA-N tetrahydrofuran Natural products C=1C=COC=1 YLQBMQCUIZJEEH-UHFFFAOYSA-N 0.000 description 1
- 238000012719 thermal polymerization Methods 0.000 description 1
- 229920002803 thermoplastic polyurethane Polymers 0.000 description 1
- 239000010409 thin film Substances 0.000 description 1
- KSBAEPSJVUENNK-UHFFFAOYSA-L tin(ii) 2-ethylhexanoate Chemical compound [Sn+2].CCCCC(CC)C([O-])=O.CCCCC(CC)C([O-])=O KSBAEPSJVUENNK-UHFFFAOYSA-L 0.000 description 1
- DVKJHBMWWAPEIU-UHFFFAOYSA-N toluene 2,4-diisocyanate Chemical compound CC1=CC=C(N=C=O)C=C1N=C=O DVKJHBMWWAPEIU-UHFFFAOYSA-N 0.000 description 1
Classifications
-
- C—CHEMISTRY; METALLURGY
- C08—ORGANIC MACROMOLECULAR COMPOUNDS; THEIR PREPARATION OR CHEMICAL WORKING-UP; COMPOSITIONS BASED THEREON
- C08G—MACROMOLECULAR COMPOUNDS OBTAINED OTHERWISE THAN BY REACTIONS ONLY INVOLVING UNSATURATED CARBON-TO-CARBON BONDS
- C08G18/00—Polymeric products of isocyanates or isothiocyanates
- C08G18/06—Polymeric products of isocyanates or isothiocyanates with compounds having active hydrogen
- C08G18/08—Processes
- C08G18/0895—Manufacture of polymers by continuous processes
-
- B—PERFORMING OPERATIONS; TRANSPORTING
- B29—WORKING OF PLASTICS; WORKING OF SUBSTANCES IN A PLASTIC STATE IN GENERAL
- B29C—SHAPING OR JOINING OF PLASTICS; SHAPING OF MATERIAL IN A PLASTIC STATE, NOT OTHERWISE PROVIDED FOR; AFTER-TREATMENT OF THE SHAPED PRODUCTS, e.g. REPAIRING
- B29C48/00—Extrusion moulding, i.e. expressing the moulding material through a die or nozzle which imparts the desired form; Apparatus therefor
- B29C48/001—Combinations of extrusion moulding with other shaping operations
- B29C48/0012—Combinations of extrusion moulding with other shaping operations combined with shaping by internal pressure generated in the material, e.g. foaming
-
- C—CHEMISTRY; METALLURGY
- C08—ORGANIC MACROMOLECULAR COMPOUNDS; THEIR PREPARATION OR CHEMICAL WORKING-UP; COMPOSITIONS BASED THEREON
- C08G—MACROMOLECULAR COMPOUNDS OBTAINED OTHERWISE THAN BY REACTIONS ONLY INVOLVING UNSATURATED CARBON-TO-CARBON BONDS
- C08G18/00—Polymeric products of isocyanates or isothiocyanates
- C08G18/06—Polymeric products of isocyanates or isothiocyanates with compounds having active hydrogen
- C08G18/28—Polymeric products of isocyanates or isothiocyanates with compounds having active hydrogen characterised by the compounds used containing active hydrogen
- C08G18/67—Unsaturated compounds having active hydrogen
- C08G18/675—Low-molecular-weight compounds
-
- C—CHEMISTRY; METALLURGY
- C08—ORGANIC MACROMOLECULAR COMPOUNDS; THEIR PREPARATION OR CHEMICAL WORKING-UP; COMPOSITIONS BASED THEREON
- C08G—MACROMOLECULAR COMPOUNDS OBTAINED OTHERWISE THAN BY REACTIONS ONLY INVOLVING UNSATURATED CARBON-TO-CARBON BONDS
- C08G18/00—Polymeric products of isocyanates or isothiocyanates
- C08G18/06—Polymeric products of isocyanates or isothiocyanates with compounds having active hydrogen
- C08G18/28—Polymeric products of isocyanates or isothiocyanates with compounds having active hydrogen characterised by the compounds used containing active hydrogen
- C08G18/67—Unsaturated compounds having active hydrogen
- C08G18/675—Low-molecular-weight compounds
- C08G18/677—Low-molecular-weight compounds containing heteroatoms other than oxygen and the nitrogen of primary or secondary amino groups
Definitions
- This invention relates to a continuous process for the bulk polymerization of polyurethanes. More specifically, it relates to the application of twin screw extruders as reactors for making radiation curable polyurethanes.
- EP-A-0 040 151 discloses thermoplastic polyurethanes which are prepared with monomers having an acrylate or methacrylate moiety but the reaction is not carried out in an extruder.
- This invention provides a process for making radiation curable polyurethanes having reactive groups by bulk polymerization in a twin screw extruder. It can be summarized as a process for bulk polymerization of polyurethanes which comprises:
- oligomeric diol means a high average molecular weight ( ⁇ 400) diol.
- the diols used may be polyester, polycarbonate, polydimethylsiloxane, or polyether diols, or dihydroxy polyolefins such as dihydroxy polybutadiene.
- the inventive process can further comprise the step of curing or cross-linking the product polymer by exposing it to radiation.
- organic diisocyanates used in the inventive process are described in general by the formula: OCNR2NCO wherein R2 is an alkylene, cycloalkylene, arylene, substituted-alkylene, substituted-cycloalkylene, substituted arylene or combinations thereof. They can include alicyclic, aliphatic and aromatic diisocyanates.
- the useful aliphatic and alicyclic diisocyanates include: 1,4-cyclohexane bis(methyleneisocyanate); dicyclohexyl methane 4,4'-diisocyanate; 1,4-cyclohexyl diisocyanate; hexamethylene diisocyanate; 1,6-diisocyanato-2,2,4,4-tetramethylhexane; 1,6-diisocyanato-2,4,4-trimethylhexane; isophorone diisocyanate; and wherein R3 is -CH3 or -C2H5.
- the useful aromatic diisocyanates include napthalene-1,5-diisocyanate, diphenylmethane-4,4'-diisocyanate, toluene diisocyanate, p-phenylene diisocyanate, dibenzyl diisocyanate, diphenyl ether diisocyanate, m- and p-tetramethylxylene diisocyanate such as are included in the general formula OCN-Ar-Y-Ar-NCO wherein Ar is cyclic, i.e.
- Y may be a carbon-to-carbon valence bond, an alkylene radical containing 1 to 5 carbon atoms, oxygen, sulfur, sulfoxide, sulfone or where R is an alkyl radical of 1 to 5 carbon atoms.
- the oligomeric diols can be diols of a polyester, polyether, silicone dial or a combination thereof, of the formula: HOR4OH wherein R4 is a polyether, polyester, polycarbonate or polydimethylsiloxane having a weight average molecular weight of 400 to 40,000.
- polyether glycol reactants are essentially linear hydroxyl containing compounds having ether linkages.
- the molecular weights preferably vary between 600 to 4,000.
- polyether glycols include hydroxyl terminated poly(propylene oxide), hydroxyl terminated poly(tetramethylene oxide), hydroxyl terminated poly(trimethylene oxide), hydroxyl terminated poly(hexamethylene oxide), hydroxyl terminated poly(ethylene oxide), and the like, of the formula HO[(CH2) n O] x1 H wherein n is an integer from 2 to 6 and x1 is an integer from 5 to 600, and substituted types such as hydroxyl terminated poly(1,2-propylene oxides), hydroxy terminated poly(1,2-butylene oxide), tetrahydrofuran and ethylene oxide copolyethers.
- polyester glycol reactants include linear polyesters having molecular weights between 400 and 10,000, and preferably 1,000 to 4,000.
- the polyesters utilized include those prepared by the polymerization of esters of aliphatic dicarboxylic acids including, for example, adipic, succinic, pimelic, suberic, azelaic, sebacic or their anhydrides.
- Aromatic dicarboxylic acids or their anhydrides or mixtures of aliphatic and aromatic dicarboxylic acids or their anhydrides may be used.
- Useful acids include aliphatic dicarboxylic acids of the formula HOOC-R5-COOH where R5 is an alkylene radical containing 1 to 10 carbon atoms, preferably 4 to 6 carbon atoms.
- the phthalic acids and their anhydrides are also useful.
- the glycols used in the preparation of the polyesters by reaction with the dicarboxylic acids are normally aliphatic diols containing between 2 and 10 carbon atoms, usually 2 to 6 carbon atoms, such as ethylene glycol propylene glycol, butanediol, hexamethylene diol, decamethylene diol, 2-ethylhexanediol, 1,6-neopentyl diol.
- polyester glycols may also include materials such as polycaprolactone diols.
- a small glycol can be part of the monomer mix.
- a small or short chain glycol is a glycol of low average molecular weight ( ⁇ 400), typically of the formula HOR6OH wherein R6 is an alkylene, cycloalkylene, arylene, substituted-alkylene, substituted-cycloalkylene, substituted-arylene or combination thereof. Examples of these are aliphatic, aromatic or ether glycols, containing 2 to 20 carbon atoms.
- Typical small glycols include ethylene diol, propylene diol, 1,6-hexanediol, 2-ethylhexanediol, 1,6-neopentyl diol, 1,4-butanediol, 2-butene-1,4-diol, diethylene glycol.
- Cycloaliphatic glycols such as cyclohexanedimethanol, and aromatic-aliphatic glycols such as bis-1,4-(hydroxyethoxy)benzene, may also be employed.
- the amount of small glycol optionally used may vary from greater than 0 to 10 moles per mole of oligomeric diol.
- Suitable additives i.e., photoinitiators or photosensitizers, ultraviolet light stabilizers and inhibitors may be compounded with the polyurethane materials.
- Suitable photoinitiators include peroxides, ketones, aldehydes, alkyl halides, organometallics, disulfides, benzoin, benzil, organic polyhalides, and inorganic ions such as ferric ion complexes.
- the polyurethanes produced by the inventive process have very good physical properties, and they have been used in the fields mentioned in the Background section above as well as other fields in which polyurethanes are used.
- This process allows for preparation of the polyurethane entirely from monomers pumped into the extruder or making a prepolymer, pumping it into the extruder, and chain extending it in the twin screw extruder.
- the reactions can be catalyzed or uncatalyzed.
- the catalyst is normally a tin reagent such as dibutyl tin dilaurate or stannous octoate, preferably in amounts from 10.01 to 10 phr (parts by weight per 100 parts by weight resin).
- the twin screw extruder used should have relatively close clearance between the screw flight lands and the barrel, typical values being in the range of 0.25 to 0.5 mm. It can be either a corotating or counter-rotating twin screw apparatus.
- the extruder has been found to be such a good mixer that it is unnecessary to make a premix of the raw materials fed to the extruder inlet or to use kneading elements in the extruder.
- a 34 mm diameter, counter-rotating twin screw extruder made by Leistritz GmBH of Nurnberg, West Germany was used as the extruder reactor. It had a length to diameter ratio (L/D) of 35.
- the extruder screws comprised a number of separate sections which fit onto a common drive shaft. The screws could be disassembled and rearranged in various orders and orientations. The screws may have one pitch at the inlet section, another pitch in the middle of the screw length and another pitch toward the exit end of the extruder.
- the barrel was divided into sections each of which could be either a heating section (i.e., a heating jacket) or a cooling section (i.e., jacket for circulating coolant). Consequently, one can control reaction temperature by adjustment of the temperatures of these zones.
- a typical extruder barrel temperature is about 200° C.
- the temperature in three of the 10 zones in the Leistritz apparatus was sometimes raised to about 250° C.
- the extruder typically has several addition ports down its length, one can add reagents at several points along the reaction path. For instance, very sensitive reagents could be added closer to the exit of the extruder.
- the ability to keep the double bonds from the acrylate or methacrylate groups from reacting in the extruder is dependent on concentration and the use of stabilizers.
- concentration of this extender in the reacting mass within the extruder at any given time should be no more than about five weight percent.
- Chemical free radical polymerization stabilizers e.g., p-methoxyphenol
- Residence time distribution of the reactants in the twin screw extruder reactor is changed by the geometry of the reactor (e.g., screw geometry), the chemistry of the reaction itself, the temperatures at which the extruder barrel sections are controlled, and the rotational speed of the extruder screws. Typical residence times are less than 10 minutes.
- IPNs interpenetrating polymer networks
- the term IPN denotes a class of materials which contain at least two polymers, each in network form. The two polymers must have been synthesized or crosslinked in the presence of each other, and they cannot be physically separated. IPNs may be thought of as two polymer networks which have been interwoven or which have become inextricably tangled together in three dimensions. IPNs have a unique set of physical properties often different from the properties of either constituent polymer itself.
- a monoacrylate or polyacrylate can be added to the twin screw extruder at a zone near the discharge end, for example the seventh zone, to obtain mixing without premature acrylate polymerization.
- Example 11 teaches how to make an IPN by this process.
- the twin screw extruder had ten 120 mm zones which were configured as follows: Zone Screw Pitch Feed 12 mm transitioning to 6 mm single start helix 1 6 mm single start helix 2 6 mm single start helix 3 6 mm single start helix 4 6 mm single start helix 5 6 mm single start helix 6 6 mm single start helix 7 first 90 mm - 6 mm single start helix, last 30 mm - 30 mm triple start helix 8 30 mm triple start helix 9 first 30 mm - 30 mm triple start helix, last 90 mm - 6 mm single start helix There was also a heated end block or connecting zone.
- Diols and isocyanate reactants were maintained in individual storage tanks under a nitrogen atmosphere and the reactants pumped into the first zone of the extruder by means of two gear pumps in series in each feed line.
- a homogeneous diol feed was achieved by heating a mixture of the various components to approximately 55° C and mixing. The diol feed was maintained at 55° C and stirred throughout the extrusion run.
- the extrudate was fed directly into a die pump, which helped control pressures at the discharge of the extruder, which was, in turn, connected to a film die (30.5 cm wide) by means of a neck tube.
- a die pump which helped control pressures at the discharge of the extruder, which was, in turn, connected to a film die (30.5 cm wide) by means of a neck tube.
- a film die (30.5 cm wide) by means of a neck tube.
- Each of the ten zones of the extruder as well as the die pump, the neck tube and the film die were maintained at a nominal 200° C throughout extrusion of the polyurethane material.
- the extruder speed was set at 28 - 31 rpm and the diol and isocyanate feeds adjusted to provide a NCO/OH moles per minute feed ratio of 1.02 at a total flow rate of 40 grams per minute with the die pump operating at 7 - 7.2 rpm.
- An approximately 6 mil (152 micrometer) thick film of the polyurethane was extruded onto a single coated silicone release paper on a chilled (20° C) collector roll.
- the cross-linkable polyurethane film was soluble in dimethyl acetamide (DMAc) but after exposure to E-beam irradiation (5 megarads at 150 kV under a nitrogen purge at a rate of about 7.6 meters per minute) the film was insoluble.
- DMAc dimethyl acetamide
- a control sample of polyurethane film of identical composition except that it contained no 2-GMA did not cross-link on exposure to an equivalent E-beam irradiation as is evidenced by the fact that it remained soluble in DMAc after irradiation.
- a film prepared from a solution blend of the same control sample and approximately 1 percent 2-GMA monomer did not cross-link and become insoluble in DMAc after exposure to comparable E-beam irradiation.
- Example 2 The procedure described in Example 1 was used to prepare a 6 mil (152 »m) thick cross-linkable polyurethane film from a Desmodur W® isocyanate feed and the following diol feed:
- Weight Percent Reactant 85.58 PTMO 1000 10.97 1,4 - Butane Diol 1.56 2 - Glyceryl Methacrylate 0.79 Tinuvin 770® 0.79 Tinuvin 328® 0.08 Dibutyl Tin Dilaurate 0.08 p - Methoxyphenol 0.16 Benzoin sec-Butyl Ether8 8. Available from Aldrich Chemicals, Milwaukee, WI.
- the extruder speed was set at 30 rpm and the diol and isocyanate feeds adjusted to provide a NCO/OH moles per minute feed ratio of 1.02 at a total flow rate of 40 grams per minute with the die pump operating at 7.2 rpm.
- the film produced from this composition was cross-linked by passing it through a RPC Industries UV Processor (Plainfield IL) equipped with medium pressure UV lamps operating at 400 volts and 7.5 amps at a rate of about 9 meters per minute under a nitrogen atmosphere.
- the cross-linked film was insoluble in DMAc.
- Weight Percent Reactant 85.49 PTMO 1000 11.22 1,4 - Butane Diol 1.55 2 -N',N'-[bis-2-hydroxyethylureido]ethyl methacrylate9 0.79 Tinuvin 770® 0.79 Tinuvin 328® 0.08 Dibutyl Tin Dilaurate 0.08 p - Methoxyphenol 9.
- the extruder speed was set at 30 - 31 rpm and the diol and isocyanate feeds adjusted to provide a NCO/OH moles per minute feed ratio of 1.02 at a total flow rate of 40 grams per minute with the die pump operating at 7.2 - 7.3 rpm.
- the film die was removed for this experiment and the extrudate stream from the neck tube was directed into a water quench bath.
- the polymer filament was passed over a roll of paper toweling to partially dry it prior to pelletizing in a Con-Air Pelletizer.
- An approximately 10 mil (254 »m) thick film was prepared from the above described pellets by pressing the pellets between two pieces of polyester film at about 345 MPa pressure at 160° C. As pressed, the film was soluble in DMAc but after exposure to E-beam radiation conditions of Example 1 it was insoluble.
- a pelletized cross-linkable polyurethane was prepared according to the procedure described in EXAMPLE 3 from a Desmodur W® isocyanate feed and the following diol feed:
- Weight Percent Reactant 85.72 PTMO 1000 10.99 1,4 - Butane Diol 1.56 1 - Glyceryl Methacrylate10 0.79 Tinuvin 770® 0.79 Tinuvin 328® 0.08 Dibutyl Tin Dilaurate 0.08 p - Methoxyphenol 10. Prepared according to the procedure described in U.S. Patent No. 3,957,362.
- the extruder speed was set at 30 rpm and the diol and isocyanate feeds adjusted to provide a NCO/OH moles per minute feed ratio of 1.02 to 1.03 at a total flow rate of 40 grams per minute with the die pump operating at 7.2 rpm.
- An approximately 10 mil (254 »m) thick film was prepared from the above described pellets by pressing the pellets between two pieces of polyester film at about 34.5 MPa at 160° C. As pressed, the film was soluble in DMAc but after exposure to E-beam radiation as above it was insoluble.
- a pelletized cross-linkable polyurethane was prepared according to the procedure described in EXAMPLE 3 from a Desmodur W® isocyanate feed and the following diol feed:
- the extruder speed was set at 30 rpm and the diol and isocyanate feeds adjusted to provide a NCO/OH moles per minute feed ratio of 1.02 at a total flow rate of 40 grams per minute with the die pump operating at about 7 rpm.
- An approximately 250 »m (10 mil) thick film was prepared from the above described pellets by pressing the pellets between two pieces of polyester film at about 34.5 MPa at 160° C. As pressed, the film was soluble in DMAc but after exposure to E-beam radiation conditions of Example 1 it was insoluble.
- a pelletized cross-linkable polyurethane was prepared according to the procedure described in EXAMPLE 3 from a Desmodur W® isocyanate feed and the following diol feed:
- the extruder speed was set at 36 - 41 rpm and the diol and isocyanate feeds adjusted to provide a NCO/OH moles per minute feed ratio of 1.0 at an initial total flow rate of 40 grams per minute with the die pump operating at 6.8 - 7.2 rpm.
- the feed pump speeds were then adjusted to maintain the same NCO/OH feed ratio but a total flow rate of 80 grams per minute with an extruder speed of 63 rpm and the die pump operating at 14 - 14.9 rpm.
- An approximately 250 »m (10 mil) thick film was prepared from the above described pellets by pressing the pellets between two pieces of polyester film at about 34.5 MPa at 160° C. As pressed, the film was soluble in DMAc but after exposure to E-beam radiation conditions of Example 1 it was insoluble.
- a pelletized cross-linkable polyurethane was prepared according to the procedure described in Example 3 from a Desmodur W® isocyanate feed and the following diol feed:
- the extruder speed was set at 50 rpm and the diol and isocyanate feeds adjusted to provide a NCO/OH moles per minute feed ratio of 1.00-1.02 at a total flow rate of 40 grams per minute with the die pump operating at 6.8 rpm.
- An approximately 250 »m (10 mil) thick film was prepared from the above described pellets by pressing the pellets between two pieces of polyester film at about 34.5 MPa at 160° C. As pressed, the film was soluble in DMAc but after exposure to E-beam radiation conditions of Example 1 it was insoluble.
- a pelletized cross-linkable polyurethane was prepared according to the procedure described in Example 3 from the following diol and isocyanate feeds:
- Weight Percent Reactant 83.62 PTMO 1000 13.17 1,4 - Butane Diol 1.52 2 - Glyceryl Methacrylate 0.77 Tinuvin 770® 0.77 Tinuvin 328® 0.08 Dibutyl Tin Dilaurate 0.08 p - Methoxyphenol
- An approximately 250 »m (10 mil) thick film was prepared from the above described pellets by pressing the pellets between two pieces of polyester film at about 34.5 MPa at 160° C. As pressed, the film was soluble in DMAc but after exposure to E-beam radiation conditions of Example 1 it was insoluble.
- a pelletized cross-linkable polyurethane was prepared according to the procedure described in Example 3 from a Desmodur W® isocyanate feed and the following diol feed:
- the extruder speed was set at 30-46 rpm and the diol and isocyanate feeds adjusted to provide a NCO/OH moles per minute feed ratio of 0.98-1.017 at a total flow rate of 40 grams per minute with the die pump operating at 7.3 rpm. Little if any reaction occurred at these conditions as judged by a large isocyanate peak in the infrared spectrum of the extrudate, so an additional 5 grams of dimethyl tin dilaurate was added to the diol feed and the temperature of zones 3 - 5 increased to a nominal 230° C.
- An approximately 250 »m (10 mil) thick film was prepared from the above described pellets by pressing the pellets between two pieces of polyester film at about 34.5 MPa at 160° C. As pressed, the film was soluble in DMAc but after exposure to E-beam radiation conditions of Example 1 it was insoluble.
- the extruder speed was set at 100 rpm and the diol and isocyanate feeds adjusted to provide a NCO/OH moles per minute feed ratio of 1.025 at a total flow rate of 40 grams per minute with the die pump operating at 7.2 - 7.4 rpm.
- 2 - glyceryl methacrylate was added to the diol feed tank to provide a nominal 1.92 weight percent 2-GMA content in the diol feed and the diol and isocyanate feeds adjusted to provide a NCO/OH moles per minute feed ratio of 1.025.
- the final composition of the three films was as follows: Final Film Composition Reactant Nominal 2-GMA (0.5 %) Content (1.0 %) In Film (3.0 %) PTMO 1000 39.50 38.98 37.00 1,4 - Butane Diol 12.10 11.95 11.33 2 - Glyceryl Methacrylate 0.50 1.00 2.83 Dibutyl Tin Dilaurate 0.05 0.05 0.05 p - Methoxyphenol 0.05 0.05 0.05 0.05 0.05 0.05 Desmodur W® 47.90 48.00 48.75
- the mechanical properties of the cross-linked films demonstrate that strength of the films is maintained at a high level over the compositional range investigated but, as the 2-GMA content of the film increases, the elongation of the film decreases.
- Example 2 A procedure similar to that described in Example 1 except that the extruder was equipped with a Ruska positive displacement pump feeding into zone 7, and the extrudate stream was collected in aluminum trays and was used to prepare cross-linkable polyurethane filaments containing nominally 10 and 20 weight percent cyclohexyl methacrylate.
- the polymer was prepared from a Desmodur W® isocyanate feed and the following diol feed:
- the extruder speed was set at 28 rpm and the diol and isocyanate feeds adjusted to provide a NCO/OH moles per minute feed ratio of 1.0 at a total flow rate of 40 grams per minute with the die pump operating at 7.0 rpm.
- cyclohexyl methacrylate feed rate was adjusted to deliver the cyclohexyl methacrylate into the polyurethane filament at a nominal 20 weight percent level (total flow rate on addition of the cyclohexyl methacrylate increased to 48 grams per minute).
- the two polyurethane filaments were cut into pellets and pressed into films approximately 125 »m (5 mils) thick by pressing the pellets between polyester film at about 34.5 MPa at 120° C. As pressed, the films were soluble in DMAc, but after two passes through a RPC UV Processor under conditions described in Example 2, the film having 10 weight percent cyclohexyl methacrylate was insoluble in DMAc while the film containing 20 weight percent cyclohexyl methacrylate was still soluble. Both types of film (10 and 20% cyclohexyl methacrylate) were exposed to 5 Mrads electron beam dose (200 KV at 7.6 m/min. under N2 atmosphere) after which both were found to be insoluble in DMAc at 100° C.
- substantially complete as used with reference to completion of diisocyanate reaction means that no more than 0.7 weight percent diisocyanate remains in the product. This quantity could be found by infrared analysis, assuming that the residual isocyanate is all attributable to the monomeric species.
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Description
- This invention relates to a continuous process for the bulk polymerization of polyurethanes. More specifically, it relates to the application of twin screw extruders as reactors for making radiation curable polyurethanes.
- The synthesis of polyurethanes using extruder reactors is known to the art. Also, there are known various radiation curable polyurethanes, e.g., polyurethanes which cross link under the influence of ultraviolet or electron beam radiation. Such polymers are potentially useful in several fields, such as magnetic recording tape binders; automobile body protective coverings; wound management materials; and high moisture vapor transmission films. However, although the advantages of continuous processing in an extruder reactor (e.g., the ability to modify the polymer on line without stopping the process) are known, the necessary elevated temperature and shear conditions within an extruder have led to the belief that radiation curable functionalities such as acrylates would not survive the extrusion process.
- It is well known in the art that the acrylate type double bond is very susceptible to polymerization either by free radical initiator or by thermal polymerization, as pointed out in Odian, G., Principles of Polymerization, John Wiley & Sons, New York, 1981, p. 214; and Kirk-Othmer Encyclopaedia of Chemical Technology, Third Ed., Vol. 1, John Wiley & Sons, New York, p. 349. EP-A-0 040 151 discloses thermoplastic polyurethanes which are prepared with monomers having an acrylate or methacrylate moiety but the reaction is not carried out in an extruder.
- This invention provides a process for making radiation curable polyurethanes having reactive groups by bulk polymerization in a twin screw extruder. It can be summarized as a process for bulk polymerization of polyurethanes which comprises:
- (A) providing the following raw materials:
- (1) at least one diisocyanate;
- (2) at least one oligomeric or polymeric diol having a molecular weight of from 400 to 40,000; and
- (3) at least one chain extending monomer having an acrylate or methacrylate moiety selected from the
monomers having the formulas:
m = 0-4
n₁ = 1-4
R₁ is -H or -CH₃
R₇ is -H, -CH₃, or -C₂H₅
A is
Y is ―N〈, ―O―C〈̶R₇, or ―SC〈̶R₇
and optionally further providing - (4) a short chain glycol selected from aliphatic, cycloaliphatic and aromatic glycols having a molecular weight less than 400;
- (B) continuously conveying the above raw materials to a twin screw extruder and reacting them together to the desired degree of conversion in the extruder while conveying the reacting mass through the extruder under the following conditions:
- (1) molar ratio of isocyanate to hydroxy moieties 1.00 ± 0.05;
- (2) ratio of chain extending monomer to other monomers sufficient to yield a polymer product having such chain extender incorporated therein to a level of from 0.1 to less than 10 weight percent;
- (3) concentration of chain extending monomer within reacting mass in the extruder is no greater than 5 weight percent;
- (4) extruder barrel temperature of at least 185°C and sufficient to initiate and maintain reaction between the raw materials; and
- (5) extruder configured to have a residence time sufficient to obtain substantially complete reaction of the diisocyanate indicated by ≦ 0.7 weight percent diisocyanate in the product as measured by infrared spectrometry of the extrudate; and
- (C) cooling the result product polymer from the discharge of the extruder;
- (i) weight average molecular weight greater than 80,000; and
- (ii) acrylate or methacrylate functionality in the polymer molecule resulting from the chain extending monomer and which functionality survived the extruder reaction conditions.
- 1. narrow molecular weight distribution or polydispersity (p) or Mw/Mn, typically less than 3;
- 2. radiation (ultraviolet or electron beam) curable, the cured polymers being insoluble in organic solvents in which polyurethanes are commonly soluble;
- 3. high tensile strength.
- The term "oligomeric diol" means a high average molecular weight (≧400) diol. The diols used may be polyester, polycarbonate, polydimethylsiloxane, or polyether diols, or dihydroxy polyolefins such as dihydroxy polybutadiene.
- The inventive process can further comprise the step of curing or cross-linking the product polymer by exposing it to radiation.
- The organic diisocyanates used in the inventive process are described in general by the formula:
OCNR₂NCO
wherein
R₂ is an alkylene, cycloalkylene, arylene, substituted-alkylene, substituted-cycloalkylene, substituted arylene or combinations thereof. They can include alicyclic, aliphatic and aromatic diisocyanates. The useful aliphatic and alicyclic diisocyanates include:
1,4-cyclohexane bis(methyleneisocyanate); dicyclohexyl methane 4,4'-diisocyanate; 1,4-cyclohexyl diisocyanate; hexamethylene diisocyanate;
1,6-diisocyanato-2,2,4,4-tetramethylhexane; 1,6-diisocyanato-2,4,4-trimethylhexane; isophorone diisocyanate; and
wherein R₃ is -CH₃ or -C₂H₅. - The useful aromatic diisocyanates include napthalene-1,5-diisocyanate, diphenylmethane-4,4'-diisocyanate, toluene diisocyanate, p-phenylene diisocyanate, dibenzyl diisocyanate, diphenyl ether diisocyanate, m- and p-tetramethylxylene diisocyanate such as are included in the general formula
OCN-Ar-Y-Ar-NCO
wherein Ar is cyclic, i.e. an arylene radical, and Y may be a carbon-to-carbon valence bond, an alkylene radical containing 1 to 5 carbon atoms, oxygen, sulfur, sulfoxide, sulfone or
where R is an alkyl radical of 1 to 5 carbon atoms. - The oligomeric diols can be diols of a polyester, polyether, silicone dial or a combination thereof, of the formula:
HOR₄OH wherein R₄ is a polyether, polyester,
polycarbonate or polydimethylsiloxane having a weight average molecular weight of 400 to 40,000. - Representative polyether glycol reactants, also termed poly(alkylene oxides), are essentially linear hydroxyl containing compounds having ether linkages. The molecular weights preferably vary between 600 to 4,000. Examples of polyether glycols include hydroxyl terminated poly(propylene oxide), hydroxyl terminated poly(tetramethylene oxide), hydroxyl terminated poly(trimethylene oxide), hydroxyl terminated poly(hexamethylene oxide), hydroxyl terminated poly(ethylene oxide), and the like, of the formula HO[(CH₂)nO]x1H wherein n is an integer from 2 to 6 and x₁ is an integer from 5 to 600, and substituted types such as hydroxyl terminated poly(1,2-propylene oxides), hydroxy terminated poly(1,2-butylene oxide), tetrahydrofuran and ethylene oxide copolyethers.
- Representative polyester glycol reactants include linear polyesters having molecular weights between 400 and 10,000, and preferably 1,000 to 4,000. The polyesters utilized include those prepared by the polymerization of esters of aliphatic dicarboxylic acids including, for example, adipic, succinic, pimelic, suberic, azelaic, sebacic or their anhydrides. Aromatic dicarboxylic acids or their anhydrides or mixtures of aliphatic and aromatic dicarboxylic acids or their anhydrides may be used. Useful acids include aliphatic dicarboxylic acids of the formula HOOC-R₅-COOH where R₅ is an alkylene radical containing 1 to 10 carbon atoms, preferably 4 to 6 carbon atoms. The phthalic acids and their anhydrides are also useful. The glycols used in the preparation of the polyesters by reaction with the dicarboxylic acids are normally aliphatic diols containing between 2 and 10 carbon atoms, usually 2 to 6 carbon atoms, such as ethylene glycol propylene glycol, butanediol, hexamethylene diol, decamethylene diol, 2-ethylhexanediol, 1,6-neopentyl diol.
- Representative polyester glycols may also include materials such as polycaprolactone diols.
-
-
- In addition to the diisocyanate, oligomeric diol and chain extending acrylate or methacrylate, a small glycol can be part of the monomer mix. A small or short chain glycol is a glycol of low average molecular weight (<400), typically of the formula
HOR₆OH
wherein R₆ is an alkylene, cycloalkylene, arylene, substituted-alkylene, substituted-cycloalkylene, substituted-arylene or combination thereof. Examples of these are aliphatic, aromatic or ether glycols, containing 2 to 20 carbon atoms. Typical small glycols include ethylene diol, propylene diol, 1,6-hexanediol, 2-ethylhexanediol, 1,6-neopentyl diol, 1,4-butanediol, 2-butene-1,4-diol, diethylene glycol. Cycloaliphatic glycols such as cyclohexanedimethanol, and aromatic-aliphatic glycols such as bis-1,4-(hydroxyethoxy)benzene, may also be employed. The amount of small glycol optionally used may vary from greater than 0 to 10 moles per mole of oligomeric diol. - Suitable additives, i.e., photoinitiators or photosensitizers, ultraviolet light stabilizers and inhibitors may be compounded with the polyurethane materials. Suitable photoinitiators include peroxides, ketones, aldehydes, alkyl halides, organometallics, disulfides, benzoin, benzil, organic polyhalides, and inorganic ions such as ferric ion complexes.
- In general, the process steps can be performed as follows:
- 1. Diisocyanate and/or oligomeric diol capped with a diisocyanate is provided in a first vessel.
- 2. A mixture of at least one oligomeric diol and the chain extending acrylate or methacrylate monomer, plus any desired additives, the short chain diol, additional chain extenders, and catalysts is made in a second vessel.
- 3. The diisocyanate and/or diisocyanate prepolymer and the mixture from 2. are pumped to the inlet end of the twin screw extruder.
- 4. Typically, a positive displacement pump (e.g., Zenith® die pump) is used at the discharge of the extruder to convey the extrudate to a quench bath.
- 5. The polymer extrudate is conveyed through the quench bath which can comprise a long rectangular tank containing water or another suitable cooling fluid such as an inert, non-polar, high boiling organic liquid.
- 6. The cooled polymer strand or film is dried, for example by an air stream or by passing over paper towels.
- 7. The dried polymer strand or film is reduced to a convenient form (e.g., by a pelletizer). The polymer can be made in a variety of forms, for example thin film, rod stock, fibers, tubes or blown microfibers.
- The polyurethanes produced by the inventive process have very good physical properties, and they have been used in the fields mentioned in the Background section above as well as other fields in which polyurethanes are used. This process allows for preparation of the polyurethane entirely from monomers pumped into the extruder or making a prepolymer, pumping it into the extruder, and chain extending it in the twin screw extruder.
- The reactions can be catalyzed or uncatalyzed. When catalyzed, the catalyst is normally a tin reagent such as dibutyl tin dilaurate or stannous octoate, preferably in amounts from 10.01 to 10 phr (parts by weight per 100 parts by weight resin).
- The twin screw extruder used should have relatively close clearance between the screw flight lands and the barrel, typical values being in the range of 0.25 to 0.5 mm. It can be either a corotating or counter-rotating twin screw apparatus. The extruder has been found to be such a good mixer that it is unnecessary to make a premix of the raw materials fed to the extruder inlet or to use kneading elements in the extruder.
- In the research and development work which led to this invention, a 34 mm diameter, counter-rotating twin screw extruder made by Leistritz GmBH of Nurnberg, West Germany was used as the extruder reactor. It had a length to diameter ratio (L/D) of 35. The extruder screws comprised a number of separate sections which fit onto a common drive shaft. The screws could be disassembled and rearranged in various orders and orientations. The screws may have one pitch at the inlet section, another pitch in the middle of the screw length and another pitch toward the exit end of the extruder.
- In addition, the barrel was divided into sections each of which could be either a heating section (i.e., a heating jacket) or a cooling section (i.e., jacket for circulating coolant). Consequently, one can control reaction temperature by adjustment of the temperatures of these zones. A typical extruder barrel temperature is about 200° C. The temperature in three of the 10 zones in the Leistritz apparatus was sometimes raised to about 250° C.
- Since the extruder typically has several addition ports down its length, one can add reagents at several points along the reaction path. For instance, very sensitive reagents could be added closer to the exit of the extruder.
- The ability to keep the double bonds from the acrylate or methacrylate groups from reacting in the extruder (yielding a substantially gel free polymer) is dependent on concentration and the use of stabilizers. Although the process allows making a polymer with up to 10 percent (meth)acrylate containing chain extender, the concentration of this extender in the reacting mass within the extruder at any given time should be no more than about five weight percent. In order to stay below that concentration yet reach a ratio of more than 5% in the product, it is possible to feed the (meth)acrylate containing chain extender to the extruder at more than one point along the extruder by feed ports down the barrel. Chemical free radical polymerization stabilizers (e.g., p-methoxyphenol) can also influence relative reactivity of the (meth)acrylate moieties.
- Residence time distribution of the reactants in the twin screw extruder reactor is changed by the geometry of the reactor (e.g., screw geometry), the chemistry of the reaction itself, the temperatures at which the extruder barrel sections are controlled, and the rotational speed of the extruder screws. Typical residence times are less than 10 minutes.
- The following additional parameters are typical of the process:
- 1) Attempt to operate the twin screw extruder in order to maximize current flow to the extruder motor (amps) because this condition indicates maximizing molecular weight.
- 2) Run the twin screw extruder full.
- 3) Feed the raw materials to the extruder feed zone at a pressure of about 69 kPa.
- A further aspect of the invention is the formation of interpenetrating polymer networks (IPNs). The term IPN denotes a class of materials which contain at least two polymers, each in network form. The two polymers must have been synthesized or crosslinked in the presence of each other, and they cannot be physically separated. IPNs may be thought of as two polymer networks which have been interwoven or which have become inextricably tangled together in three dimensions. IPNs have a unique set of physical properties often different from the properties of either constituent polymer itself. In order to make an IPN, a monoacrylate or polyacrylate can be added to the twin screw extruder at a zone near the discharge end, for example the seventh zone, to obtain mixing without premature acrylate polymerization. Example 11 teaches how to make an IPN by this process.
- The invention will be further clarified by consideration of the following Examples which are intended to be purely exemplary.
- In all of the examples, if the water content of the PTMO 1000 and 1,4 - butane diol was above 0.05 weight percent, it was reduced to below that level by heating the materials to 110° C with agitation in a closed vessel while pulling a vacuum of 10 mm or less for a period of 3 hours. If the water level remained above 0.05% after this dehydration operation, the procedure was repeated a second time for a period of 2 hours.
- The twin screw extruder had ten 120 mm zones which were configured as follows:
Zone Screw Pitch Feed 12 mm transitioning to 6 mm single start helix 1 6 mm single start helix 2 6 mm single start helix 3 6 mm single start helix 4 6 mm single start helix 5 6 mm single start helix 6 6 mm single start helix 7 first 90 mm - 6 mm single start helix, last 30 mm - 30 mm triple start helix 8 30 mm triple start helix 9 first 30 mm - 30 mm triple start helix, last 90 mm - 6 mm single start helix
There was also a heated end block or connecting zone. - Diols and isocyanate reactants were maintained in individual storage tanks under a nitrogen atmosphere and the reactants pumped into the first zone of the extruder by means of two gear pumps in series in each feed line. A homogeneous diol feed was achieved by heating a mixture of the various components to approximately 55° C and mixing. The diol feed was maintained at 55° C and stirred throughout the extrusion run.
- The extrudate was fed directly into a die pump, which helped control pressures at the discharge of the extruder, which was, in turn, connected to a film die (30.5 cm wide) by means of a neck tube. Each of the ten zones of the extruder as well as the die pump, the neck tube and the film die were maintained at a nominal 200° C throughout extrusion of the polyurethane material.
-
Weight Percent Reactant 85.72 PTMO 1000¹ 10.99 1,4 - Butane Diol² 1.56 2 - Glyceryl Methacrylate³ 0.79 Tinuvin 770®⁴ 0.79 Tinuvin 328®⁵ 0.08 Dibutyl Tin Dilaurate⁶ 0.08 p - Methoxyphenol⁷ 1. Polytetramethylene Oxide (MW approx. 1000). 2. Available from GAF Corp., Wayne, NJ. 3. 2-GMA, preparation described in US Pat. No. 4,578,504. 4. Bis-(2,2,6,6-tetramethyl-4-piperidyl)sebacate, available from Ciba Geigy Corp., Plastics and Additives Div., Hawthorne, NY. 5. 2-(2'-Hydroxy-3',5'-di-tert-amylphenyl)benzotriazole, available from Ciba Geigy Corp., Plastics and Additives Div., Hawthorne, NY. 6. Available from M & T Chemicals, Rahway, NJ. 7. MEHQ, available from J.T. Baker Chemical Co., Phillipsburg, NJ. -
- Desmodur W® -
- H₁₂MDI, Dicyclohexylmethane - 4,4' - Diisocyanate, MW 262, available from Mobay Corp., Pittsburg, PA.
- The extruder speed was set at 28 - 31 rpm and the diol and isocyanate feeds adjusted to provide a NCO/OH moles per minute feed ratio of 1.02 at a total flow rate of 40 grams per minute with the die pump operating at 7 - 7.2 rpm. An approximately 6 mil (152 micrometer) thick film of the polyurethane was extruded onto a single coated silicone release paper on a chilled (20° C) collector roll.
- As extruded, the cross-linkable polyurethane film was soluble in dimethyl acetamide (DMAc) but after exposure to E-beam irradiation (5 megarads at 150 kV under a nitrogen purge at a rate of about 7.6 meters per minute) the film was insoluble. A control sample of polyurethane film of identical composition except that it contained no 2-GMA did not cross-link on exposure to an equivalent E-beam irradiation as is evidenced by the fact that it remained soluble in DMAc after irradiation. Similarly, a film prepared from a solution blend of the same control sample and approximately 1 percent 2-GMA monomer did not cross-link and become insoluble in DMAc after exposure to comparable E-beam irradiation.
- The procedure described in Example 1 was used to prepare a 6 mil (152 »m) thick cross-linkable polyurethane film from a Desmodur W® isocyanate feed and the following diol feed:
-
Weight Percent Reactant 85.58 PTMO 1000 10.97 1,4 - Butane Diol 1.56 2 - Glyceryl Methacrylate 0.79 Tinuvin 770® 0.79 Tinuvin 328® 0.08 Dibutyl Tin Dilaurate 0.08 p - Methoxyphenol 0.16 Benzoin sec-Butyl Ether⁸ 8. Available from Aldrich Chemicals, Milwaukee, WI. - The extruder speed was set at 30 rpm and the diol and isocyanate feeds adjusted to provide a NCO/OH moles per minute feed ratio of 1.02 at a total flow rate of 40 grams per minute with the die pump operating at 7.2 rpm.
- The film produced from this composition was cross-linked by passing it through a RPC Industries UV Processor (Plainfield IL) equipped with medium pressure UV lamps operating at 400 volts and 7.5 amps at a rate of about 9 meters per minute under a nitrogen atmosphere. The cross-linked film was insoluble in DMAc.
- A procedure similar to that described in Example 1 was used to prepare cross-linkable polyurethane pellets from a Desmodur W® isocyanate feed and the following diol feed:
-
Weight Percent Reactant 85.49 PTMO 1000 11.22 1,4 - Butane Diol 1.55 2 -N',N'-[bis-2-hydroxyethylureido]ethyl methacrylate⁹ 0.79 Tinuvin 770® 0.79 Tinuvin 328® 0.08 Dibutyl Tin Dilaurate 0.08 p - Methoxyphenol 9. Prepared by reacting isocyanato ethyl methacrylate and N,N -bis-(2-hydroxyethyl) amine. - The extruder speed was set at 30 - 31 rpm and the diol and isocyanate feeds adjusted to provide a NCO/OH moles per minute feed ratio of 1.02 at a total flow rate of 40 grams per minute with the die pump operating at 7.2 - 7.3 rpm.
- The film die was removed for this experiment and the extrudate stream from the neck tube was directed into a water quench bath. The polymer filament was passed over a roll of paper toweling to partially dry it prior to pelletizing in a Con-Air Pelletizer.
- An approximately 10 mil (254 »m) thick film was prepared from the above described pellets by pressing the pellets between two pieces of polyester film at about 345 MPa pressure at 160° C. As pressed, the film was soluble in DMAc but after exposure to E-beam radiation conditions of Example 1 it was insoluble.
- A pelletized cross-linkable polyurethane was prepared according to the procedure described in EXAMPLE 3 from a Desmodur W® isocyanate feed and the following diol feed:
-
Weight Percent Reactant 85.72 PTMO 1000 10.99 1,4 - Butane Diol 1.56 1 - Glyceryl Methacrylate¹⁰ 0.79 Tinuvin 770® 0.79 Tinuvin 328® 0.08 Dibutyl Tin Dilaurate 0.08 p - Methoxyphenol 10. Prepared according to the procedure described in U.S. Patent No. 3,957,362. - The extruder speed was set at 30 rpm and the diol and isocyanate feeds adjusted to provide a NCO/OH moles per minute feed ratio of 1.02 to 1.03 at a total flow rate of 40 grams per minute with the die pump operating at 7.2 rpm.
- An approximately 10 mil (254 »m) thick film was prepared from the above described pellets by pressing the pellets between two pieces of polyester film at about 34.5 MPa at 160° C. As pressed, the film was soluble in DMAc but after exposure to E-beam radiation as above it was insoluble.
- A pelletized cross-linkable polyurethane was prepared according to the procedure described in EXAMPLE 3 from a Desmodur W® isocyanate feed and the following diol feed:
-
Weight Percent Reactant 85.64 PTMO 1000 11.07 1,4 - Butane Diol 1.56 Mono Methacrylate of Trimethylol Ethane¹¹ 0.79 Tinuvin 770® 0.79 Tinuvin 328® 0.08 Dibutyl Tin Dilaurate 0.08 p - Methoxyphenol 11. Prepared using a procedure similar to that described in US Pat. No. 3,210,327. - The extruder speed was set at 30 rpm and the diol and isocyanate feeds adjusted to provide a NCO/OH moles per minute feed ratio of 1.02 at a total flow rate of 40 grams per minute with the die pump operating at about 7 rpm.
- An approximately 250 »m (10 mil) thick film was prepared from the above described pellets by pressing the pellets between two pieces of polyester film at about 34.5 MPa at 160° C. As pressed, the film was soluble in DMAc but after exposure to E-beam radiation conditions of Example 1 it was insoluble.
- A pelletized cross-linkable polyurethane was prepared according to the procedure described in EXAMPLE 3 from a Desmodur W® isocyanate feed and the following diol feed:
-
Weight Percent Reactant 86.81 PTMO 1000 11.46 1,4 - Butane Diol 1.50 Monoacrylate of Trimethylol Ethane¹¹ 0.08 Dibutyl Tin Dilaurate 0.08 p - Methoxyphenol 11. Prepared using a procedure similar to that described in US Pat. No. 3,210,327. - The extruder speed was set at 36 - 41 rpm and the diol and isocyanate feeds adjusted to provide a NCO/OH moles per minute feed ratio of 1.0 at an initial total flow rate of 40 grams per minute with the die pump operating at 6.8 - 7.2 rpm. The feed pump speeds were then adjusted to maintain the same NCO/OH feed ratio but a total flow rate of 80 grams per minute with an extruder speed of 63 rpm and the die pump operating at 14 - 14.9 rpm.
- An approximately 250 »m (10 mil) thick film was prepared from the above described pellets by pressing the pellets between two pieces of polyester film at about 34.5 MPa at 160° C. As pressed, the film was soluble in DMAc but after exposure to E-beam radiation conditions of Example 1 it was insoluble.
- A pelletized cross-linkable polyurethane was prepared according to the procedure described in Example 3 from a Desmodur W® isocyanate feed and the following diol feed:
-
Weight Percent Reactant 83.44 Rucoflex S102-55®¹² 13.35 1,4 - Butane Diol 1.52 2 - Glyceryl Methacrylate 0.77 Tinuvin 770® 0.77 Tinuvin 328® 0.08 Dibutyl Tin Dilaurate 0.08 p - Methoxyphenol 12. A hydroxy terminated butylene adipate polyester copolymer, MW 1975.35, available from Ruco Polymer Corp., Hicksville, NY. - The extruder speed was set at 50 rpm and the diol and isocyanate feeds adjusted to provide a NCO/OH moles per minute feed ratio of 1.00-1.02 at a total flow rate of 40 grams per minute with the die pump operating at 6.8 rpm.
- An approximately 250 »m (10 mil) thick film was prepared from the above described pellets by pressing the pellets between two pieces of polyester film at about 34.5 MPa at 160° C. As pressed, the film was soluble in DMAc but after exposure to E-beam radiation conditions of Example 1 it was insoluble.
- A pelletized cross-linkable polyurethane was prepared according to the procedure described in Example 3 from the following diol and isocyanate feeds:
-
Weight Percent Reactant 83.62 PTMO 1000 13.17 1,4 - Butane Diol 1.52 2 - Glyceryl Methacrylate 0.77 Tinuvin 770® 0.77 Tinuvin 328® 0.08 Dibutyl Tin Dilaurate 0.08 p - Methoxyphenol -
- Isophorone Diisocyanate -
- MW 222.28, available from Muddex Inc., Piscataday, NJ.
- Because isophorone diisocyanate is significantly less reactive than H₁₂MDI (Desmodur W)® the temperature of the feed zone and zones 1 - 3 was increased to a nominal 240 - 250° C and the temperature of zones 4 - 9 was maintained at a nominal 200° C for this experiment. The extruder speed was set at 45 - 47 rpm and the diol and isocyanate feeds adjusted to provide a NCO/OH moles per minute feed ratio of 1.017 at a total flow rate of 40 grams per minute with the die pump operating at 6.8 rpm.
- An approximately 250 »m (10 mil) thick film was prepared from the above described pellets by pressing the pellets between two pieces of polyester film at about 34.5 MPa at 160° C. As pressed, the film was soluble in DMAc but after exposure to E-beam radiation conditions of Example 1 it was insoluble.
- A pelletized cross-linkable polyurethane was prepared according to the procedure described in Example 3 from a Desmodur W® isocyanate feed and the following diol feed:
-
Weight Percent Reactant 79.64 PTMO 1000 12.54 1,4 - Butane Diol 1.45 1 - Glyceryl Methacrylate 4.76 Oligomeric Dimethacrylate¹³ 0.73 Tinuvin 770® 0.73 Tinuvin 328® 0.07 Dimethyl Tin Dilaurate¹⁴ 0.07 p - Methoxyphenol 13. Prepared by adding hydroxyethyl methacrylate to PCA5-1, a polytetramethylene oxide capped with H₁₂MDI (available from Polymethane Specialities Co., Inc., Lindhurst, NJ) and heating at 70° C with stirring under a N₂ atmosphere for 2 hours. 14. Available from Witco Chemicals, New York, NY. - The extruder speed was set at 30-46 rpm and the diol and isocyanate feeds adjusted to provide a NCO/OH moles per minute feed ratio of 0.98-1.017 at a total flow rate of 40 grams per minute with the die pump operating at 7.3 rpm. Little if any reaction occurred at these conditions as judged by a large isocyanate peak in the infrared spectrum of the extrudate, so an additional 5 grams of dimethyl tin dilaurate was added to the diol feed and the temperature of zones 3 - 5 increased to a nominal 230° C. The amperage draw decreased at these conditions so the temperature of zones 3 - 5 was increased a second time to a nominal 250° C which brought the amperage draw to 2 amps and decreased the isocyanate peak in the infrared spectrum of the extrudate, indicative of reaction between the diols and isocyanate.
- An approximately 250 »m (10 mil) thick film was prepared from the above described pellets by pressing the pellets between two pieces of polyester film at about 34.5 MPa at 160° C. As pressed, the film was soluble in DMAc but after exposure to E-beam radiation conditions of Example 1 it was insoluble.
- A procedure similar to that described in Example 1 except that the extruder screw configuration consisted of a 6 mm single start helix in zones 1 - 9; and the film was extruded directly into a water quench tank was used to prepare three approximately 12 mil (304 »m) thick polyurethane cross- linkable films having nominal 2-GMA concentrations of 0.5, 1.0 and 3.0 weight percent from a Desmodur W® isocyanate feed and the following initial diol feed:
-
Weight Percent Reactant 75.67 PTMO 1000 23.18 1,4 - Butane Diol 0.96 2 - Glyceryl Methacrylate 0.1 Dibutyl Tin Dilaurate 0.1 p - Methoxyphenol - The extruder speed was set at 100 rpm and the diol and isocyanate feeds adjusted to provide a NCO/OH moles per minute feed ratio of 1.025 at a total flow rate of 40 grams per minute with the die pump operating at 7.2 - 7.4 rpm.
- After approximately 2.5 hours, 2 - glyceryl methacrylate was added to the diol feed tank to provide a nominal 1.92 weight percent 2-GMA content in the diol feed and the diol and isocyanate feeds adjusted to provide a NCO/OH moles per minute feed ratio of 1.025.
- After approximately another 2.5 hours, a second addition of 2-GMA to the diol feed was made to provide a nominal 5.52 weight percent 2-GMA content in the diol feed and the isocyanate and diol feeds adjusted to provide a NCO/OH moles per minute feed ratio of 1.025.
- The final composition of the three films was as follows:
Final Film Composition Reactant Nominal 2-GMA (0.5 %) Content (1.0 %) In Film (3.0 %) PTMO 1000 39.50 38.98 37.00 1,4 - Butane Diol 12.10 11.95 11.33 2 - Glyceryl Methacrylate 0.50 1.00 2.83 Dibutyl Tin Dilaurate 0.05 0.05 0.05 p - Methoxyphenol 0.05 0.05 0.05 Desmodur W® 47.90 48.00 48.75 - As extruded, all three film samples were soluble in DMAc but after exposure to E-beam irradiation (5 megarads at 300 KV under a N₂ atmosphere at a rate of about 7.6 meters per minute) the films were all insoluble in DMAc. Mechanical properties (stress at break and elongation) of the uncross-linked and cross-linked films as determined using an Instron Model TTCH Test Apparatus (available from Instron Engineering Corp., Canton, MA) at a cross-head rate of 20 cm/minute were:
Film Mechanical Properties Sample (Wt. % 2-GMA) Stress at Break (MPa) Elongation at Break (%) 0.5 68.28 300 0.5 (X-LKD) 59.31 280 1.0 72.41 320 1.0 (X-LKD) 73.10 300 3.0 73.10 320 3.0 (X-LKD) 58.62 240 - The mechanical properties of the cross-linked films demonstrate that strength of the films is maintained at a high level over the compositional range investigated but, as the 2-GMA content of the film increases, the elongation of the film decreases.
- A procedure similar to that described in Example 1 except that the extruder was equipped with a Ruska positive displacement pump feeding into zone 7, and the extrudate stream was collected in aluminum trays and was used to prepare cross-linkable polyurethane filaments containing nominally 10 and 20 weight percent cyclohexyl methacrylate. The polymer was prepared from a Desmodur W® isocyanate feed and the following diol feed:
-
Weight Percent Reactant 85.36 PTMO 1000 11.21 1,4 - Butane Diol 1.55 2 - Glyceryl Methacrylate 0.79 Tinuvin 770® 0.79 Tinuvin 328® 0.08 Dibutyl Tin Dilaurate 0.08 p - Methoxyphenol 0.16 Benzoin sec-Butyl Ether - The extruder speed was set at 28 rpm and the diol and isocyanate feeds adjusted to provide a NCO/OH moles per minute feed ratio of 1.0 at a total flow rate of 40 grams per minute with the die pump operating at 7.0 rpm. After the system had stabilized (approximately 1/4 hour) the temperature in zones 7 - 9 and the end block was reduced to a nominal 185° C and cyclohexyl methacrylate (available from Polysciences, Inc., Worthington PA) introduced into zone 7 of the extruder using the Ruska pump, adjusting the pump speed to deliver the cyclohexyl methacrylate into the polyurethane filament at a nominal 10 weight percent level (total flow rate on addition of the cyclohexyl methacrylate increased to 44 grams per minute).
- After approximately an additional 1/2 hour the cyclohexyl methacrylate feed rate was adjusted to deliver the cyclohexyl methacrylate into the polyurethane filament at a nominal 20 weight percent level (total flow rate on addition of the cyclohexyl methacrylate increased to 48 grams per minute).
- The two polyurethane filaments were cut into pellets and pressed into films approximately 125 »m (5 mils) thick by pressing the pellets between polyester film at about 34.5 MPa at 120° C. As pressed, the films were soluble in DMAc, but after two passes through a RPC UV Processor under conditions described in Example 2, the film having 10 weight percent cyclohexyl methacrylate was insoluble in DMAc while the film containing 20 weight percent cyclohexyl methacrylate was still soluble. Both types of film (10 and 20% cyclohexyl methacrylate) were exposed to 5 Mrads electron beam dose (200 KV at 7.6 m/min. under N₂ atmosphere) after which both were found to be insoluble in DMAc at 100° C.
- The term substantially complete as used with reference to completion of diisocyanate reaction means that no more than 0.7 weight percent diisocyanate remains in the product. This quantity could be found by infrared analysis, assuming that the residual isocyanate is all attributable to the monomeric species.
Reactive extrusion allows one to prepare polymer in the extruder and extrude it in the final desired form. Both aliphatic and aromatic polyurethanes having the following characteristics (in addition to those listed above) can be made in this way:
The polymers may be considered block copolymers.
Claims (9)
- A process for bulk polymerization of polyurethanes which comprises:(A) providing the following raw materials:(1) at least one diisocyanate;(2) at least one oligomeric or polymeric diol having a molecular weight of from 400 to 40,000; and(3) at least one chain extending monomer having an acrylate or methacrylate moiety selected from the
monomers having the formulas:
m = 0-4
n₁ = 1-4
R₁ is -H or -CH₃
R₇ is -H, -CH₃, or -C₂H₅
A is
Y is ―N〈, ―O―C〈̶R₇, or ―SC〈̶R₇
and optionally further providing(4) a short chain glycol selected from aliphatic, cycloaliphatic and aromatic glycols having a molecular weight less than 400;(B) continuously conveying the above raw materials to a twin screw extruder and reacting them together to the desired degree of conversion in the extruder while conveying the reacting mass through the extruder under the following conditions:(1) molar ratio of isocyanate to hydroxy moieties 1.00 ± 0.05;(2) ratio of chain extending monomer to other monomers sufficient to yield a polymer product having such chain extender incorporated therein to a level of from 0.1 to less than 10 weight percent;(3) concentration of chain extending monomer within reacting mass in the extruder is no greater than 5 weight percent;(4) extruder barrel temperature of at least 185°C and sufficient to initiate and maintain reaction between the raw materials; and(5) extruder configured to have a residence time sufficient to obtain substantially complete reaction of the diisocyanate indicated by ≦ 0.7 weight percent diisocyanate in the product as measured by infrared spectrometry of the extrudate; and(C) cooling the result product polymer from the discharge of the extruder;
to yield a polyurethane having the following properties:(i) weight average molecular weight greater than 80,000; and(ii) acrylate or methacrylate functionality in the polymer molecule resulting from the chain extending monomer and which functionality survived the extruder reaction conditions. - The process of Claim 1 which further comprises curing the product polymer by exposing it to radiation.
- The process of Claim 1 wherein a prepolymer of the diisocyanate and the oligomeric or polymeric diol is made before step (B).
- The process of Claim 1 wherein the diisocyanate is selected from: aliphatic diisocyanates selected from hexamethylene diisocyanate;
1,6-diisocyanato-2,2,4,4-tetramethylhexane; 1,6-diisocyanato-2,4,4-trimethylhexane; diisocyanates with the formula
R₃ is -CH₃ or C₂H₅;
alicyclic diisocyanates selected from 1,4-cyclohexane bis(methyleneisocyanate); dicyclohexylmethane 4,4' diisocyanate; 1,4-cyclohexyl diisocyanate; isophorone diisocyanate; and aromatic diisocyanates having the formula OCN-Ar-Y-Ar-NCO wherein Ar is an arylene radical, and Y may be a carbon-to-carbon valence bond, an alkylene radical containing 1 to 5 carbon atoms, oxygen, sulfur, sufoxide,
sulfone or - The process of claim 1 wherein the oligomeric or polymeric diol is selected from linear hydroxyl containing compounds having the following formula
HO[(CH₂)nO]x1H wherein n is an integer from 2 to 6 and x₁ is an integer from 5 to 600; hydroxyl terminated poly(1,2-propylene oxides); hydroxy terminated poly(1,2-butylene oxide); hydroxy-substituted tetrahydrofuran and ethylene oxide copolyethers;
polyesters prepared by polymerization of esters of dicarboxylic acids or their anhydrides with at least one glycol having 2-10 carbon atoms; and silicone diols having the formula - The process of Claim 1 wherein the short chain diol is selected from ethylene diol, propylene diol, 1,6-hexanediol, 2-ethylhexanediol,
1,6-neopentyl diol, 1,4-butanediol, 2-butene-1,4-diol, diethylene glycol, cyclohexanedimethanol, and bis-1,4-(hydroxyethoxy)benzene. - The process of claim 1 wherein the amount of short chain diol used is from greater than 0 to 10 moles per mole of oligomeric or polymeric diol.
- The process of Claim 2 which further comprises making an interpenetrating polymer network by adding to the twin screw extruder near the discharge end a monomer selected from acrylates and methacrylates.
- A process according to Claim 1 for bulk polymerization of polyurethanes which comprises:(A) providing the following raw materials:(1) at least one diisocynate;(2) at least one oligomeric or polymeric diol having a molecular weight of from 400 to 40,000; and(3) at least one chain extending monomer having an acrylate or methacrylate moiety selected from the
monomers having the formulas:
m = 0-4
n₁ = 1-4
R₁ is -H or -CH₃
R₇ is -H, -CH₃, or -C₂H₅,
A is
Y is ―N〈, ―O―C〈̶R₇, or ―SC〈̶R₇
and optionally further providing(4) a short chain glycol selected from aliphatic, cycloaliphatic and aromatic glycols having a molecular weight less than 400;(B) continuously conveying the above raw materials to a twin screw extruder and reacting them together to the desired degree of conversion in the extruder while conveying the reacting mass through the extruder under the following conditions:(1) molar ratio of isocyanate to hydroxy moieties 1.00 ± 0.05;(2) ratio of chain extending monomer to other monomers sufficient to yield a polymer product having such chain extender incorporated therein to a level of from 0.1 to less than 10 weight percent;(3) concentration of chain extending monomer within reacting mass in the extruder is no greater than 5 weight percent;(4) extruder barrel temperature of at least 185°C and sufficient to initiate and maintain reaction between the raw materials; and(5) extruder configured to have a residence time sufficient to obtain substantially complete reaction of the diisocyanate indicated by ≦ 0.7 weight percent diisocyanate in the product as measured by infrared spectrometry of the extrudate; and(C) cooling the result product polymer from the discharge of the extruder;
to yield a polyurethane having the following properties:(i) weight average molecular weight greater than 80,000; and(ii) acrylate or methacrylate functionality in the polymer molecule resulting from the chain extending monomer and which functionality survived the extruder reaction conditions.
Applications Claiming Priority (2)
Application Number | Priority Date | Filing Date | Title |
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US263713 | 1988-10-28 | ||
US07/263,713 US4948859A (en) | 1988-10-28 | 1988-10-28 | Extruder polymerization of polyurethanes |
Publications (3)
Publication Number | Publication Date |
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EP0367445A2 EP0367445A2 (en) | 1990-05-09 |
EP0367445A3 EP0367445A3 (en) | 1990-07-18 |
EP0367445B1 true EP0367445B1 (en) | 1995-12-13 |
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EP (1) | EP0367445B1 (en) |
JP (1) | JP2617585B2 (en) |
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AU (1) | AU619593B2 (en) |
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US6464713B2 (en) * | 1990-06-28 | 2002-10-15 | Peter M. Bonutti | Body tissue fastening |
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-
1988
- 1988-10-28 US US07/263,713 patent/US4948859A/en not_active Expired - Lifetime
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1989
- 1989-09-20 CA CA000612067A patent/CA1308851C/en not_active Expired - Fee Related
- 1989-09-25 AU AU41755/89A patent/AU619593B2/en not_active Ceased
- 1989-10-18 DE DE68925101T patent/DE68925101T2/en not_active Expired - Fee Related
- 1989-10-18 ES ES89310721T patent/ES2080753T3/en not_active Expired - Lifetime
- 1989-10-18 EP EP89310721A patent/EP0367445B1/en not_active Expired - Lifetime
- 1989-10-26 JP JP1279630A patent/JP2617585B2/en not_active Expired - Fee Related
- 1989-10-27 KR KR1019890015476A patent/KR0141492B1/en not_active IP Right Cessation
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EP0367445A2 (en) | 1990-05-09 |
KR0141492B1 (en) | 1998-07-01 |
ES2080753T3 (en) | 1996-02-16 |
US4948859A (en) | 1990-08-14 |
JPH02170816A (en) | 1990-07-02 |
JP2617585B2 (en) | 1997-06-04 |
DE68925101D1 (en) | 1996-01-25 |
EP0367445A3 (en) | 1990-07-18 |
AU619593B2 (en) | 1992-01-30 |
CA1308851C (en) | 1992-10-13 |
DE68925101T2 (en) | 1996-08-22 |
KR900006387A (en) | 1990-05-08 |
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